CN106607025B - Isobutane dehydrogenation catalyst and preparation method thereof - Google Patents

Isobutane dehydrogenation catalyst and preparation method thereof Download PDF

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CN106607025B
CN106607025B CN201510689722.7A CN201510689722A CN106607025B CN 106607025 B CN106607025 B CN 106607025B CN 201510689722 A CN201510689722 A CN 201510689722A CN 106607025 B CN106607025 B CN 106607025B
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catalyst
isobutane dehydrogenation
dehydrogenation catalyst
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CN106607025A (en
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姜冬宇
吴文海
樊志贵
曾铁强
缪长喜
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Sinopec Shanghai Research Institute of Petrochemical Technology
China Petrochemical Corp
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China Petrochemical Corp
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Abstract

The invention relates to an isobutane dehydrogenation catalyst and a preparation method thereof, and mainly solves the problems of low activity and poor stability of a dehydrogenation catalyst prepared in the prior art. The isobutane dehydrogenation catalyst prepared by the invention comprises the following components in parts by weight: a)0.1-5 parts of Pt or its oxide; b)0.1 to 5 parts of rare earth metal or oxide thereof c)0.1 to 5 parts of Sn or oxide thereof; d)0.1-10 parts of AB with spinel structure2O4A is selected from at least one of divalent metal cations, B is selected from at least one of trivalent metal cations; e)80-99 parts of carrier Al2O3The technical scheme better solves the problem and can be used in the industrial production of the catalyst for preparing isobutene by isobutane dehydrogenation.

Description

Isobutane dehydrogenation catalyst and preparation method thereof
Technical Field
The invention relates to a catalyst for preparing isobutene by isobutane dehydrogenation and a preparation method thereof.
Background
In recent years, with the rapid development of petrochemical industry and polymer industry, the demand of olefin is increasing day by day, among C4 resources rich in China, oil field butane usually contains 20% -40% of isobutane, while the utilization rate of C4 fraction in China is very low, and most of the C4 fraction is directly consumed as fuel except for a small amount of C4 fraction used for alkylation. Isobutene is an important chemical raw material and is mainly used for producing polyisobutylene, butyl rubber and methyl tert-butyl ether (MTBE), the MTBE is a high-octane liquid and is often used as an additive for improving the octane number of gasoline, the market demand is large, and the contradiction of isobutene resource shortage is more prominent. The method for preparing isobutene by dehydrogenating isobutane as a raw material can improve the utilization value of isobutane and relieve the shortage problem of isobutene in China. Isobutane dehydrogenation is a strongly endothermic reaction and only at relatively high reaction temperatures is it possible to obtain the desired olefin yields. However, an excessively high reaction temperature often causes a series of side reactions, thereby reducing the selectivity of olefin, causing rapid carbon deposition and deactivation on the surface of the catalyst, and causing problems of poor performance and low selectivity of the catalyst, and therefore, it is necessary to prepare a dehydrogenation catalyst with excellent performance, and to improve the conversion rate of alkane and the selectivity of olefin.
At present, the industrialized isobutane dehydrogenation technology comprises an oop Oleflex technology, a Lummus Catofin technology, a Uhde STAR technology, a Linde PDH technology, a Snamprogetti-Yarsintez co-developed FBD technology and the like, wherein the industrialized devices are mostly the Oleflex technology and the Catofin technology, catalysts applied by the Oleflex technology and the cambogetti technology are respectively a Pt catalyst and a Cr catalyst, and the Pt catalyst is a research hotspot due to the characteristics of high activity, low pollution, low wear rate and the like. Recently, there have been many reports on Pt-based catalysts for isobutane dehydrogenation, and Wan et al, Industral&"fluorescence of Lanthantum Addition on Catalytic Properties of PtSnK/Al" published in Engineering Chemistry Research 2011,50:4280-2O3Catalyst for Isobutane Dehydrogenation "(addition of La to PtSnK/Al)2O3The influence of the catalytic performance of isobutane dehydrogenation) is shown in the characterization of the article, the addition of a proper amount of La can reduce the carbon deposition amount of the catalyst and improve the dispersion degree of Pt, and the effects of Sn and a carrier are also enhanced, so that Sn exists in an oxidation state, and the stability of the catalyst is improved. The preferred content of La is 0.9%, at which point the initial conversion can reach 49% and the selectivity is greater than 95%. When La is excessive, Pt aggregates and Sn also becomes a metal, resulting in a decrease in catalyst activity. Zhang et al, Fuel Processing Technology 2012, 96: 220-supplement 227 published on "Effect of Zinc Addition on Catalytic Properties of PtSnK/gamma-Al2O3Catalyst for Isobutane Dehydrogenation "(addition of Zn for Dehydrogenation of Isobutane PtSnK/gamma)-Al2O3Influence of catalytic performance of catalyst) to research the addition of Zn auxiliary agent on PtSnK/gamma-Al2O3The influence of isobutane dehydrogenation performance shows that a proper amount of Zn can not only improve the dispersion degree of Pt, but also reduce carbon deposit. Zn enhances the effects of the Sn component and the carrier, and prevents the reduction of Sn. When the addition amount of Zn is 0.4 wt%, the isobutane conversion rate and stability are excellent, the initial conversion rate is 37%, the selectivity is 97%, and the conversion rate still has a space for improvement. Kobayashi et al, Applied Catalysis A: General 2012,417: 306-2O3-Al2O3catalst "(Fe oxide vs. Pt/Fe)2O3-Al2O3Influence of isobutane dehydrogenation reaction on catalyst) the composite oxide support Fe was studied2O3-Al2O3The dehydrogenation performance of the Pt-Sn loaded isobutane is found through research: when Fe2O3When the mass fraction is 7%, the inactivation of the catalyst is relieved, the activity of the catalyst is good, the initial conversion rate can reach 50%, and the conversion rate after 5h of reaction is achieved>40% and selectivity 95%. The strong acid sites in the catalyst are reduced due to the addition of Fe, the carbon deposit of the catalyst is less, and Fe and Pt in the catalyst can form an alloy, so that the electron density of Pt is increased.
The catalyst for preparing isobutene by isobutane dehydrogenation has been greatly developed, but the problems of low conversion rate or low olefin selectivity under the condition of high conversion rate still exist, and the stability needs to be further enhanced. The invention adopts AB2O4Spinel and rare earth elements are taken as auxiliary agents, and the surface characteristics of the catalyst can be changed by adding the spinel and the rare earth elements into the catalyst so as to improve the performance of the catalyst, so that the spinel and the rare earth elements have a good application prospect, and no related report exists at present.
Disclosure of Invention
One of the technical problems to be solved by the invention is the problems of low activity and poor stability of the isobutane dehydrogenation catalyst in the prior art, and the invention provides a novel catalyst for isobutane dehydrogenation. The second technical problem to be solved by the present invention is to provide a method for preparing a catalyst corresponding to the first technical problem.
In order to solve one of the above technical problems, the technical scheme adopted by the invention is as follows: the catalyst for isobutane dehydrogenation comprises the following components in parts by weight:
a)0.1-5 parts of Pt or its oxide;
b)0.1-5 parts of rare earth metal or oxide thereof;
c)0.1 to 5 parts of Sn or an oxide thereof;
d)0.1-10 parts of AB with spinel structure2O4A is selected from at least one of divalent metal cations, B is selected from at least one of trivalent metal cations;
e)80-99 parts of carrier Al2O3。
In the technical scheme, the preferable range of the parts of Pt or the oxides thereof is 0.1-2.5 parts by weight; the preferable range of the parts of the rare earth metal or the oxide thereof is 0.5-2 parts; the preferable range of the Sn or the oxide thereof is 0.1 to 2.5 parts; AB2O4The preferable range of the spinel part number is 1-5, A is selected from at least one of divalent metal cations, B is selected from at least one of trivalent metal cations; a is preferably at least one of Mg or Zn, B is preferably at least one of Al or Fe; the preferred composition of the spinel component, in terms of mole ratios, is Mg in a: zn is (0.25-4): 1, Al in B: fe is (0.25-4): 1; al (Al)2O3Is gamma, delta and theta type Al2O3One or two of the above-mentioned materials, and its carrier also contains 0.1-1 portion of TiO2Or ZrO2. In terms of molar ratio, the ratio of Pt to Sn in the catalyst is (0.01-5): 1.
to solve the second technical problem, the invention adopts the following technical scheme: a catalyst for preparing isobutene by isobutane dehydrogenation and a preparation method thereof comprise the following steps:
a) weighing Al in required content2O3Pouring into deionized water, stirring, weighing soluble salts A and B with required content, respectively dissolving in deionized water, mixing, and pouring into mixture of carrier and waterContinuously stirring, and slowly dripping ammonia water under continuous stirring until the pH value is 7-10; aging the product, filtering and washing to obtain a filter cake, drying and roasting to obtain AB2O4And Al2O3The composite carrier of (1);
b) dissolving a required amount of soluble salt of Sn in a proper amount of hydrochloric acid solution, adding the soluble salt into the composite carrier obtained in the step a under stirring, uniformly mixing, and dipping, drying and roasting to obtain a catalyst precursor I;
c) dissolving Pt and soluble salt of rare earth metal with required amount in a proper amount of water, adding the catalyst precursor I obtained in the step b under stirring, uniformly mixing, and dipping, drying and roasting to obtain the catalyst for preparing isobutene by dehydrogenating isobutane.
In the technical scheme, the dipping temperature in the dipping process is 10-80 ℃, the dipping time is 1-24 hours, the drying temperature is 80-150 ℃, and the drying time is 6-24 hours. The roasting process is carried out for 6-24 hours at the temperature of 450-650 ℃.
In the technical scheme, the soluble salt of the rare earth metal, A and B can be selected from one of chloride, nitrate or acetate; the soluble salt of Pt is preferably chloroplatinic acid; the soluble salt of tin is selected from stannous chloride or stannic chloride.
The catalyst prepared by the method is subjected to activity evaluation in an isothermal fixed bed reactor, and for evaluating a system for preparing isobutene by dehydrogenating isobutane, the process is briefly described as follows:
the flow of isobutane raw material gas is regulated through a mass flow meter, the isobutane raw material gas enters a preheating zone to be mixed, then the isobutane raw material gas enters a reaction zone, the preheating zone and the reaction zone of a reactor are heated by electric heating wires to reach a preset temperature, and the inner diameter of the reactor is a stainless steel sleeve with phi 9 mm-phi 6mm, and the length of the stainless steel sleeve is about 400 mm. The reacted gas was passed through a condensing pot and then analyzed for composition by gas chromatography. The catalyst evaluation conditions in the isothermal fixed bed reactor were as follows: about 0.5g of catalyst is loaded into an isothermal reactor with an internal diameter of phi 9mm to phi 6mm (the height of the catalyst bed is about 17mm), and the volume ratio of isobutane to hydrogen is 10: 1-1: 1, the reaction temperature is 400-600 ℃, and the reaction pressure is 0-1 MPaThe mass space velocity of the isobutane is 3.0-8.0 h-1And the reaction raw material is in contact reaction with the catalyst to obtain isobutene.
Pure Pt-Sn/Al during dehydrogenation of isobutane2O3The catalyst has strong surface acidity, and the deactivation speed is accelerated because the carbon is easily deposited on the surface of the catalyst. In order to slow down the deactivation speed of the catalyst, the performance of the catalyst can be improved by adding other auxiliary agents, and meanwhile, the reaction temperature can be reduced to reduce the carbon deposition on the surface of the catalyst. Compared with the prior art, the invention has obvious advantages and outstanding effects, the addition of the rare earth metal elements can reduce the acidity of the catalyst surface, AB2O4The addition of spinel can improve the dispersion of Pt element on the carrier or promote the formation of more active sites Pt, thereby improving the carbon deposition resistance of Pt catalysts, and enhancing the effects of Sn components and carriers, thereby improving the performance of the catalysts. The catalyst is used in the isobutane dehydrogenation reaction by adopting the evaluation conditions, and the activity evaluation result shows that the catalyst has higher alkane conversion rate, the isobutane conversion rate can reach more than 55% at lower reaction temperature, and the catalyst has higher selectivity, the isobutene selectivity is more than 94%, the catalyst conversion rate is still 53% after 20 times of carbon burning, and the selectivity is still more than 94%, so that the better technical effect is achieved.
The invention is further illustrated by the following examples.
Detailed Description
[ example 1 ]
After 9.38g of alumina carrier was weighed and poured into 200mL of deionized water and stirred for 1 hour, 1.637g of aluminum nitrate and 0.649g of zinc nitrate were weighed and dissolved in 50mL of deionized water, respectively, and then the two were mixed uniformly and poured into a mixed solution of alumina and water, and after stirring was continued for 1 hour, ammonia was slowly dropped while continuing stirring until the pH was 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain ZnAl2O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving the stannous chloride in 10mL of hydrochloric acid solution, adding the mixture into the carrier under stirring, and uniformly mixingAnd soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is recorded as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst A. The catalyst evaluation conditions were as follows: 0.5g of catalyst is loaded into the isothermal fixed bed reactor (the height of a catalyst bed layer is 17mm), the reaction is carried out under normal pressure and at the temperature of 550 ℃; isobutane to hydrogen volume ratio 2.5: 1; the mass space velocity of isobutane is 4.6h-1. The results are shown in Table 2.
[ example 2 ]
9.77g of alumina carrier is weighed and poured into 200mL of deionized water to be stirred for 1 hour, 0.041g of aluminum nitrate and 0.017g of zinc nitrate are weighed and respectively dissolved in 50mL of deionized water, then the two are uniformly mixed and poured into the mixed solution of the alumina and the water, after stirring for 1 hour, ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain ZnAl2O4-Al2O3And (3) a carrier. 0.295g of stannic chloride is weighed, dissolved in 10mL of hydrochloric acid solution, added to the carrier under stirring, mixed uniformly, dipped at 10 ℃ for 24 hours, and then dried at 90 ℃ for 16 hours to obtain a catalyst precursor, which is recorded as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 10 ℃ for 24 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst B. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 3 ]
Weighing 8.78g of alumina carrier, pouring the alumina carrier into 200mL of deionized water, stirring for 1 hour, weighing 4.093g of aluminum nitrate and 1.623g of zinc nitrate, respectively dissolving the aluminum nitrate and the zinc nitrate into 50mL of deionized water, uniformly mixing the two, pouring the mixture into a mixed solution of alumina and water, continuously stirring for 1 hour, and slowly dropping ammonia water until the pH value is 8.5. Aging the product for 2 hr, suction filtering and washing with 2L water to obtain filter cake, and filtering the filter cakeDrying at 90 ℃ for 16 hours, and then roasting in a muffle furnace at 580 ℃ for 20 hours to obtain ZnAl2O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 80 ℃ for 1 hour, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I while stirring, uniformly mixing, soaking at 80 ℃ for 1 hour, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst C. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 4 ]
9.28g of alumina carrier is weighed and poured into 200mL of deionized water, stirred for 1 hour, 2.046g of aluminum nitrate and 0.811g of zinc nitrate are weighed and respectively dissolved in 50mL of deionized water, then the two are uniformly mixed and poured into a mixed solution of alumina and water, after stirring for 1 hour, ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 80 ℃ for 24 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain ZnAl2O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 80 ℃ for 24 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 80 ℃ for 24 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst D. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 5 ]
9.68g of alumina carrier is weighed and poured into 200mL of deionized water, stirred for 1 hour, 0.410g of aluminum nitrate and 0.162g of zinc nitrate are weighed and respectively dissolved in 50mL of deionized water, then the two are uniformly mixed and poured into a mixed solution of alumina and water, after stirring for 1 hour, ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. The product is aged for 2 hours and washed with 2L of water by suction filtrationWashing to obtain a filter cake, drying the filter cake at 150 ℃ for 6 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain ZnAl2O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 150 ℃ for 6 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 150 ℃ for 6 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst E. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 6 ]
9.38g of alumina carrier is weighed and poured into 200mL of deionized water, stirred for 1 hour, 0.897 ferric chloride and 0.226 zinc chloride are weighed and respectively dissolved in 50mL of deionized water, then the two are uniformly mixed and poured into a mixed solution of alumina and water, after stirring for 1 hour, ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain ZnFe2O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.106g of cerium chloride, dissolving in 10mL of water, adding into the I under stirring, uniformly mixing, dipping for 12 hours at 30 ℃, drying for 16 hours at 90 ℃, and roasting for 20 hours in a muffle furnace at 580 ℃, thus obtaining the isobutane dehydrogenation catalyst F. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 7 ]
Weighing 9.38g of alumina carrier, pouring the alumina carrier into 200mL of deionized water, stirring for 1 hour, weighing 2.110g of aluminum nitrate and 0.721g of magnesium nitrate, respectively dissolving the aluminum nitrate and the magnesium nitrate into 50mL of deionized water, uniformly mixing the two, pouring the mixture into a mixed solution of alumina and water, continuously stirring for 1 hour, and slowly dropping ammonia water until the pH value is 8.5. The product is processedAging for 2 hours, leaching and washing with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain MgAl2O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159G of chloroplatinic acid and 0.186G of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I while stirring, uniformly mixing, dipping for 12 hours at 30 ℃, drying for 16 hours at 90 ℃, and roasting for 20 hours in a muffle furnace at 580 ℃ to obtain the isobutane dehydrogenation catalyst G. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 8 ]
9.38g of alumina carrier is weighed and poured into 200mL of deionized water, stirred for 1 hour, then 1.616g of ferric nitrate and 0.513g of magnesium nitrate are weighed and respectively dissolved in 50mL of deionized water, then the two are uniformly mixed and poured into the mixed solution of alumina and water, after stirring for 1 hour, ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain MgFe2O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I while stirring, uniformly mixing, dipping for 12 hours at 30 ℃, drying for 16 hours at 90 ℃, and roasting for 20 hours in a muffle furnace at 580 ℃ to obtain the isobutane dehydrogenation catalyst, namely H. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 9 ]
Weighing 9.57g of alumina carrier, pouring the alumina carrier into 200mL of deionized water, stirring for 1 hour, weighing 1.412g of chromium nitrate and 0.513g of nickel nitrate, respectively dissolving the chromium nitrate and the nickel nitrate into 50mL of deionized water, uniformly mixing the chromium nitrate and the nickel nitrate, pouring the mixture into a mixed solution of alumina and water, continuously stirring for 1 hour, and slowly dripping the mixture into a mixed solution of the alumina and the water under continuous stirringAmmonia until pH 8.5. Aging the product for 1 hour, carrying out suction filtration and washing by using 1L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting in a muffle furnace at 450 ℃ for 24 hours to obtain NiCr2O4-Al2O3And (3) a carrier. Weighing 0.029g of stannic chloride, dissolving in 10mL of hydrochloric acid solution, adding the hydrochloric acid solution into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, wherein the mark is I. Weighing 0.027g of chloroplatinic acid and 0.051g of yttrium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, dipping for 12 hours at 30 ℃, drying for 16 hours at 90 ℃, and roasting for 24 hours in a muffle furnace at 450 ℃ to obtain the isobutane dehydrogenation catalyst I. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 10 ]
Weighing 8.10g of alumina carrier, pouring the alumina carrier into 200mL of deionized water, stirring for 2 hours, weighing 1.275g of gallium nitrate and 0.444g of nickel nitrate, respectively dissolving the gallium nitrate and the nickel nitrate into 50mL of deionized water, uniformly mixing the gallium nitrate and the nickel nitrate, pouring the mixture into a mixed solution of alumina and water, continuously stirring for 2 hours, and slowly dropping ammonia water until the pH value is 10. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 650 ℃ for 6 hours to obtain the NiGa2O4-Al2O3And (3) a carrier. Weighing 0.951g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is recorded as I. Weighing 1.327g of chloroplatinic acid and 2.106g of lanthanum nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 650 ℃ for 6 hours to obtain the isobutane dehydrogenation catalyst J. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 11 ]
Weighing 8.90g of alumina carrier, pouring the alumina carrier into 200mL of deionized water, stirring for 0.5 hour, weighing 1.142g of chromium nitrate and 0.440g of cadmium nitrate, respectively dissolving the chromium nitrate and the cadmium nitrate into 50mL of deionized water, uniformly mixing the chromium nitrate and the cadmium nitrate, pouring the mixture into a mixed solution of alumina and water, continuously stirring for 0.5 hour,slowly add ammonia dropwise with continued stirring until the pH is 7. Aging the product for 3 hours, filtering and washing the product by using 5L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain the CdCr2O4-Al2O3And (3) a carrier. Weighing 0.475g of stannous chloride, dissolving the stannous chloride in 10mL of hydrochloric acid solution, adding the mixture into the carrier under stirring, uniformly mixing, soaking the mixture for 12 hours at 30 ℃, and then drying the mixture for 16 hours at 90 ℃ to obtain a catalyst precursor, which is recorded as I. Weighing 0.664g of chloroplatinic acid and 0.617g of praseodymium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst K. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 12 ]
Weighing 9.39g of alumina carrier, pouring the alumina carrier into 200mL of deionized water, stirring for 1 hour, weighing 1.058g of gallium nitrate and 0.391g of cadmium nitrate, respectively dissolving the gallium nitrate and the cadmium nitrate into 50mL of deionized water, uniformly mixing the gallium nitrate and the cadmium nitrate, pouring the mixture into a mixed solution of alumina and water, continuously stirring for 1 hour, and slowly dropping ammonia water under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain the CdGa2O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. 0.159g of chloroplatinic acid and 0.094 of neodymium nitrate are weighed and dissolved in 10mL of water, added into the catalyst I under stirring, mixed uniformly, dipped for 12 hours at 30 ℃, dried for 16 hours at 90 ℃, and roasted for 20 hours in a muffle furnace at 580 ℃ to obtain the isobutane dehydrogenation catalyst L. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 13 ]
Weighing 9.38g of alumina carrier, pouring the alumina carrier into 200mL of deionized water, stirring for 1 hour, weighing 0.121g of zinc nitrate, 0.416 g of magnesium nitrate, 0.305g of aluminum nitrate and 1.312g of ferric nitrate, respectively dissolving the zinc nitrate, the magnesium nitrate, the aluminum nitrate and the ferric nitrate into 50mL of deionized water, uniformly mixing the two solutions, and pouring the mixtureAdding into the mixture of alumina and water, stirring for 1 hr, and slowly adding ammonia water under stirring until pH is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain Zn0.2Mg0.8Al0.4Fe1.6O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst M. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 14 ]
9.38g of alumina carrier is weighed and poured into 200mL of deionized water, stirred for 1 hour, then 0.509g of zinc nitrate, 0.110 g of magnesium nitrate, 1.284g of aluminum nitrate and 0.346g of ferric nitrate are weighed and respectively dissolved in 50mL of deionized water, then the two are uniformly mixed and poured into a mixed solution of alumina and water, stirring is continued for 1 hour, and ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain Zn0.8Mg0.2Al1.6Fe0.4O4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the I while stirring, uniformly mixing, dipping for 12 hours at 30 ℃, drying for 16 hours at 90 ℃, and roasting for 20 hours in a muffle furnace at 580 ℃ to obtain the isobutane dehydrogenation catalyst, wherein the N is recorded as the catalyst. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 15 ]
9.38g of oxygen were weighedAfter pouring the aluminum oxide carrier into 200mL of deionized water and stirring for 1 hour, 0.310g of zinc nitrate, 0.268 g of magnesium nitrate, 0.784g of aluminum nitrate and 0.844g of ferric nitrate are weighed and respectively dissolved in 50mL of deionized water, then the zinc nitrate and the magnesium nitrate are uniformly mixed and poured into a mixed solution of aluminum oxide and water, stirring is continued for 1 hour, and ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain Zn0.5Mg0.5AlFeO4-Al2O3And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst, namely O. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 16 ]
9.28g of alumina and 0.1g of titanium oxide carrier are weighed and poured into 200mL of deionized water, stirred for 1 hour, 1.637g of aluminum nitrate and 0.649g of zinc nitrate are respectively weighed and dissolved in 50mL of deionized water, then the two are uniformly mixed and poured into a mixed solution of alumina and water, stirring is continued for 1 hour, and ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain ZnAl2O4-Al2O3-TiO2And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst, namely P. The evaluation conditions were the same as in example 1,the results are shown in Table 2.
[ example 17 ]
9.37g of alumina and 0.01g of zirconia carrier are weighed and poured into 200mL of deionized water, stirred for 1 hour, 1.637g of aluminum nitrate and 0.649g of zinc nitrate are respectively weighed and dissolved in 50mL of deionized water, then the two are uniformly mixed and poured into a mixed solution of alumina and water, stirring is continued for 1 hour, and ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain ZnAl2O4-Al2O3-ZrO2And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst Q. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
[ example 18 ]
9.34g of alumina and 0.04g of titanium oxide carrier are weighed and poured into 200mL of deionized water, stirred for 1 hour, 1.637g of aluminum nitrate and 0.649g of zinc nitrate are respectively weighed and dissolved in 50mL of deionized water, then the two are uniformly mixed and poured into a mixed solution of alumina and water, stirring is continued for 1 hour, and ammonia water is slowly dropped under continuous stirring until the pH value is 8.5. Aging the product for 2 hours, leaching and washing the product with 2L of water to obtain a filter cake, drying the filter cake at 90 ℃ for 16 hours, and roasting the filter cake in a muffle furnace at 580 ℃ for 20 hours to obtain ZnAl2O4-Al2O3-TiO2And (3) a carrier. Weighing 0.190g of stannous chloride, dissolving in 10mL of hydrochloric acid solution, adding into the carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is marked as I. Weighing 0.159g chloroplatinic acid and 0.186g cerous nitrate in 10mL water, adding to I under stirring, mixing well, immersing at 30 deg.C for 12 hours, drying at 90 deg.C for 16 hours, and drying at 580 deg.CRoasting in a muffle furnace for 20 hours to obtain the isobutane dehydrogenation catalyst which is marked as R. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
Comparative example 1
Weighing 0.190g of stannous chloride, dissolving the stannous chloride in 10mL of hydrochloric acid solution, adding the mixture into 9.76g of alumina carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is recorded as I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I while stirring, uniformly mixing, dipping for 12 hours at 30 ℃, drying for 16 hours at 90 ℃, and roasting for 20 hours in a muffle furnace at 580 ℃ to obtain the isobutane dehydrogenation catalyst, which is marked as S. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
Comparative example 2
Weighing 0.190g of stannous chloride, dissolving the stannous chloride in 10mL of hydrochloric acid solution, adding the mixture into 9.84g of alumina carrier under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and then drying at 90 ℃ for 16 hours to obtain a catalyst precursor, which is recorded as I. Weighing 0.159g of chloroplatinic acid, dissolving in 10mL of water, adding into the I while stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst, which is marked as T. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
Comparative example 3
Preparation of a catalyst having the same composition as catalyst A, 9.36g of alumina support was added to 0.4g of ZnAl2O4The powder is stirred evenly to obtain ZnAl2O4-Al2O3And (3) a carrier. Weighing 0.19g of stannous chloride, dissolving the stannous chloride in 10mL of hydrochloric acid solution, adding 10g of the carrier while stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, and drying at 90 ℃ for 16 hours to obtain a catalyst precursor, wherein the mark is I. Weighing 0.159g of chloroplatinic acid and 0.186g of cerium nitrate, dissolving in 10mL of water, adding into the catalyst I under stirring, uniformly mixing, soaking at 30 ℃ for 12 hours, drying at 90 ℃ for 16 hours, and roasting in a muffle furnace at 580 ℃ for 20 hours to obtain the isobutane dehydrogenation catalyst U. The evaluation conditions were the same as in example 1, and the results are shown in Table 2.
TABLE 1
Figure BDA0000827316420000121
Figure BDA0000827316420000131
TABLE 2
Figure BDA0000827316420000132
Figure BDA0000827316420000141
[ examples 19 to 26 ]
The catalyst prepared in example 1 was used for dehydrogenation of isobutane under different reaction conditions, and the evaluation results are shown in table 3.
TABLE 3
Figure BDA0000827316420000142
Comparative example 4
Comparison of catalyst regeneration stability
0.5g of catalyst A, 0.5g of catalyst S, 0.5g of catalyst T and 0.5g of catalyst U were weighed out separately for evaluation of isobutane dehydrogenation, and the results after 1 hour of reaction are shown in Table 4.
TABLE 4
Figure BDA0000827316420000151

Claims (7)

1. The isobutane dehydrogenation catalyst is characterized by comprising the following components in parts by weight:
a)0.1-5 parts of Pt or its oxide;
b)0.1-5 parts of rare earth metal or oxide thereof;
c)0.1-5 parts of Sn or an oxide thereof;
d)0.1-10 parts of AB with spinel structure2O4Wherein A is selected from Mg and Zn, and B is selected from Al and Fe; composition of a in the spinel component, Mg: zn is (0.25-4): 1, the composition of B is Al: fe is (0.25-4): 1;
e)80-99 parts of carrier Al2O3。
2. The isobutane dehydrogenation catalyst according to claim 1, wherein the fraction of Pt or an oxide thereof is 0.1-2.5 parts by weight based on the weight of the isobutane dehydrogenation catalyst.
3. The isobutane dehydrogenation catalyst according to claim 1, wherein the amount of the rare earth metal or the oxide thereof is 0.5-2 parts by weight based on the parts by weight of the isobutane dehydrogenation catalyst.
4. The isobutane dehydrogenation catalyst according to claim 1, wherein the fraction of Sn or an oxide thereof is 0.1-2.5 parts by weight of the isobutane dehydrogenation catalyst.
5. Isobutane dehydrogenation catalyst according to claim 1, wherein the AB is of spinel structure2O4The weight portion of the isobutane dehydrogenation catalyst is 1-5.
6. An isobutane dehydrogenation catalyst according to claim 1, wherein said support further comprises 0.1-1 parts of TiO2Or ZrO2。
7. A process for the preparation of an isobutane dehydrogenation catalyst according to any of the claims 1-6, characterized in that it comprises the following steps:
a) weighing Al in required content2O3Pouring the mixture into a proper amount of deionized water, stirring, weighing soluble salts with required contents A and B, respectively dissolving the soluble salts in the proper amount of deionized water, uniformly mixing the soluble salts and the deionized water, pouring the mixture into a mixed solution of a carrier and water, continuously stirring, and slowly dropping ammonia water under continuous stirring until the pH value is 7-10; aging the product, filtering, washing to obtain filter cake, drying, and bakingBurning to obtain AB2O4And Al2O3The composite carrier of (1);
b) dissolving a required amount of soluble salt of Sn in a proper amount of hydrochloric acid solution, adding the soluble salt into the composite carrier obtained in the step a under stirring, uniformly mixing, and dipping, drying and roasting to obtain a catalyst precursor I;
c) dissolving Pt and soluble salt of rare earth metal with required amount in a proper amount of water, adding the catalyst precursor I obtained in the step b under stirring, uniformly mixing, and dipping, drying and roasting to obtain the isobutane dehydrogenation catalyst.
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Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102614864A (en) * 2012-03-01 2012-08-01 河南科技大学 Iso-butane dehydrogenation catalyst and preparation method thereof
CN103055857A (en) * 2011-10-24 2013-04-24 中国石油化工股份有限公司 Catalyst for low-carbon alkane dehydrogenation and preparation method thereof
CN103420769A (en) * 2012-05-16 2013-12-04 中国石油化工股份有限公司 Method for preparing low-carbon olefin from low-carbon alkane through dehydrogenation
CN104525194A (en) * 2014-12-30 2015-04-22 中国石油天然气股份有限公司 Catalyst for preparing isobutene through isobutane dehydrogenation and preparation method and application thereof

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103055857A (en) * 2011-10-24 2013-04-24 中国石油化工股份有限公司 Catalyst for low-carbon alkane dehydrogenation and preparation method thereof
CN102614864A (en) * 2012-03-01 2012-08-01 河南科技大学 Iso-butane dehydrogenation catalyst and preparation method thereof
CN103420769A (en) * 2012-05-16 2013-12-04 中国石油化工股份有限公司 Method for preparing low-carbon olefin from low-carbon alkane through dehydrogenation
CN104525194A (en) * 2014-12-30 2015-04-22 中国石油天然气股份有限公司 Catalyst for preparing isobutene through isobutane dehydrogenation and preparation method and application thereof

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
Synthesis of a structured material based on compact spheres coated with Zn or Mg spinel;Sonia Bocanegra等;《Procedia Materials Science》;20150702;第9卷;第69-78页 *

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